US20140034321A1 - Carbon Dioxide Fractionalization Process - Google Patents
Carbon Dioxide Fractionalization Process Download PDFInfo
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- US20140034321A1 US20140034321A1 US14/049,744 US201314049744A US2014034321A1 US 20140034321 A1 US20140034321 A1 US 20140034321A1 US 201314049744 A US201314049744 A US 201314049744A US 2014034321 A1 US2014034321 A1 US 2014034321A1
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Images
Classifications
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- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
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- C—CHEMISTRY; METALLURGY
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- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
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- C—CHEMISTRY; METALLURGY
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- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
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- C—CHEMISTRY; METALLURGY
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- C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
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- E—FIXED CONSTRUCTIONS
- E21—EARTH OR ROCK DRILLING; MINING
- E21B—EARTH OR ROCK DRILLING; OBTAINING OIL, GAS, WATER, SOLUBLE OR MELTABLE MATERIALS OR A SLURRY OF MINERALS FROM WELLS
- E21B43/00—Methods or apparatus for obtaining oil, gas, water, soluble or meltable materials or a slurry of minerals from wells
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- E—FIXED CONSTRUCTIONS
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- E21B43/34—Arrangements for separating materials produced by the well
- E21B43/40—Separation associated with re-injection of separated materials
Definitions
- Carbon dioxide is a naturally occurring substance in most hydrocarbon formations. While the carbon dioxide concentration will depend on the location of the formation, carbon dioxide concentrations as high as eighty percent are common in many areas, such as West Texas. Moreover, the implementation of tertiary recovery operations, such as carbon-dioxide injection into the subterranean wellbore, can increase the carbon dioxide concentration within the produced hydrocarbons. In either case, the carbon dioxide concentration of the produced hydrocarbons may be sufficiently high to require the carbon dioxide concentration to be reduced before the hydrocarbons can be refined or further processed.
- the disclosure includes a process comprising receiving a hydrocarbon feed stream comprising carbon dioxide, separating the hydrocarbon feed stream into a light hydrocarbon stream and a heavy hydrocarbon stream, separating the light hydrocarbon stream into a carbon dioxide-rich stream and a carbon dioxide-lean stream, and feeding the carbon dioxide-lean stream into a hydrocarbon sweetening process, thereby increasing the processing capacity of the hydrocarbon sweetening process compared to the processing capacity of the hydrocarbon sweetening process when fed the hydrocarbon feed stream.
- the disclosure includes an apparatus comprising a first separation unit that receives a hydrocarbon feed stream containing carbon dioxide and produces a heavy hydrocarbon stream and a light hydrocarbon stream, and a second separation unit that receives the light hydrocarbon stream and produces a carbon dioxide-rich stream and a carbon dioxide-lean stream, wherein the apparatus is configured to feed the carbon dioxide-lean stream to a physical solvent process, a membrane process, a chemical solvent process, an extractive distillation process or a carbon dioxide recovery process.
- the disclosure includes a process comprising receiving a hydrocarbon feed stream comprising carbon dioxide, cooling the hydrocarbon feed stream using a carbon dioxide-lean stream, separating the cooled hydrocarbon feed stream into a light hydrocarbon stream and a heavy hydrocarbon stream, compressing the light hydrocarbon stream, cooling the compressed light hydrocarbon stream using the carbon dioxide-lean stream, separating the compressed light hydrocarbon stream into a carbon dioxide-rich stream and the carbon dioxide-lean stream, and removing at least some of the carbon dioxide in the carbon dioxide-lean stream using a hydrocarbon sweetening process.
- FIG. 1 is a process flow diagram of one embodiment of the carbon dioxide fractionalization process.
- FIG. 2 is a process flow diagram of another embodiment of the carbon dioxide fractionalization process.
- a carbon dioxide fractionalization process that may be positioned in front of an existing hydrocarbon sweetening process to increase the processing capacity of the hydrocarbon sweetening process.
- the carbon dioxide fractionalization process purifies the hydrocarbon feed stream by removing at least some of the carbon dioxide and the heavy hydrocarbons from a hydrocarbon feed stream.
- the purification of the hydrocarbon stream reduces the carbon dioxide and heavy hydrocarbon loading on the hydrocarbon sweetening process, thereby increasing the processing capacity of the hydrocarbon sweetening process.
- the carbon dioxide fractionalization process produces a carbon dioxide-rich stream that may be injected into a subterranean formation.
- FIG. 1 illustrates one embodiment of the carbon dioxide fractionalization process 100 .
- the carbon dioxide fractionalization process 100 separates a feed mixture comprising a hydrocarbon feed stream 200 into a heavy hydrocarbon stream 254 , an acid gas stream 250 , a carbon dioxide-rich stream 244 , and a carbon dioxide-lean stream 234 , the compositions of which are discussed in detail below.
- the carbon dioxide fractionalization process 100 receives the hydrocarbon feed stream 200 and may pass the hydrocarbon feed stream 200 through a heat exchanger 102 that uses the cooled carbon dioxide-lean stream 232 to reduce the temperature of the hydrocarbon feed stream 200 .
- a first separation unit 101 that comprises one or more of a separator 108 , a reboiler 110 , a condenser 132 , and a separator 134 may then remove the heavy hydrocarbons from the cooled hydrocarbon feed stream 202 .
- the separator 108 separates the cooled hydrocarbon feed stream 202 into a bottom effluent stream 208 and a top effluent stream 214 .
- the top effluent stream 214 may then be fed into a condenser 132 , which may give off energy 312 by being cooled, and separates the top effluent stream 214 into a reflux stream 246 and a light hydrocarbon stream 248 .
- the bottom effluent stream 208 may be fed into the reboiler 110 , which may receive energy 302 by being, heated, and separates the bottom effluent stream 208 into a recycle stream 210 and a heavy hydrocarbon stream 212 .
- the heavy hydrocarbon stream 212 may then be fed into a separator 134 that separates an acid gas stream 250 from the heavy hydrocarbon stream 252 .
- the heavy hydrocarbon stream 252 may optionally be cooled by a heat exchanger 114 , for example an air cooler, to produce the heavy hydrocarbon stream 254 .
- the light hydrocarbon stream 248 may be fed into a compressor 112 that receives mechanical or electrical energy 304 and increases the pressure and/or temperature of the light hydrocarbon stream 248 , thereby creating a compressed light hydrocarbon stream 216 .
- the compressed light hydrocarbon stream 216 may then be fed into a heat exchanger 118 that uses a chilled carbon dioxide-lean stream 230 to reduce the temperature of the cooled light hydrocarbon stream 216 , thereby producing a chilled light hydrocarbon stream 224 .
- a second separation unit 103 that comprises one or more of a separator 120 , a reboiler 124 , and a condenser 122 may then remove at least some of the carbon dioxide from the chilled light hydrocarbon stream 224 .
- the separator 120 forms a first effluent leaner in carbon dioxide than the feed mixture and a second effluent richer in carbon dioxide than the feed mixture. Specifically, the separator 120 separates the chilled light hydrocarbon stream 224 into a heavy effluent stream 236 and a light effluent stream 226 .
- the light effluent stream 226 may be fed into the condenser 122 , which may give off energy 306 by being cooled, and separates the light effluent stream 226 into a condensed portion, or reflux stream 228 and the chilled carbon dioxide-lean stream 230 .
- the chilled carbon dioxide-lean stream 230 may then be passed through the heat exchangers 118 , 102 and into a hydrocarbon sweetening process 130 .
- the hydrocarbon sweetening process 130 may be any process that removes carbon dioxide from a hydrocarbon stream to make the hydrocarbon stream suitable for transportation and/or further processing. Persons of ordinary skill in the art are aware of numerous different hydrocarbon sweetening processes 130 , as illustrated by Field Processing of Petroleum, Vol. 1 : Natural Gas by Manning et al., incorporated herein by reference as if reproduced in its entirety. Several examples of the hydrocarbon sweetening process 130 are discussed in detail below.
- the heavy effluent stream 236 may be fed into the reboiler 124 , which may receive energy 308 in the form of heat, and separates the heavy effluent stream 236 into a recycle stream 238 and a cooled carbon dioxide-rich stream 240 .
- the cooled carbon dioxide-rich stream 240 may optionally be combined with the acid gas stream 250 , if desired.
- the cooled carbon dioxide-rich stream 240 may then be fed through a heat exchanger 126 that further cools the cooled carbon dioxide-rich stream 240 by removing energy 310 from the cooled carbon dioxide-rich stream 240 , thereby producing the chilled carbon dioxide-rich stream 242 .
- the chilled carbon dioxide-rich stream 242 may also be fed to a pump 128 that uses energy 314 to pump the carbon dioxide-rich stream 244 to another location, perhaps for injection into a subterranean formation.
- FIG. 2 illustrates another embodiment of the carbon dioxide fractionalization process 100 . Similar to the embodiment shown in FIG. 1 , the carbon dioxide fractionalization process 100 shown in FIG. 2 separates the hydrocarbon feed stream 200 into the heavy hydrocarbon stream 212 , the carbon dioxide-rich stream 244 , and the carbon dioxide-lean stream 234 , the compositions of which are discussed in detail below.
- the carbon dioxide fractionalization process 100 receives the hydrocarbon feed stream 200 and passes the hydrocarbon feed stream 200 through a heat exchanger 102 that uses the cooled carbon dioxide-lean stream 232 to reduce the temperature of the hydrocarbon feed stream 200 .
- the hydrocarbon feed stream is fed into the optional heat exchanger 104 , which further cools the cooled hydrocarbon feed stream 202 by removing some of its energy 300 , thereby producing a chilled hydrocarbon feed stream 202 .
- a first separation unit 101 that comprises one or more of separators 106 , 108 and the reboiler 110 may then remove the heavy hydrocarbons from the cooled chilled hydrocarbon feed stream 202 .
- the chilled hydrocarbon feed stream 202 may be fed into a separator 106 that separates the chilled hydrocarbon feed stream 202 into a light fraction 220 and a heavy fraction 206 .
- the light fraction 220 may be a vapor phase and the heavy fraction 206 may be a liquid phase.
- the light fraction 220 may be combined with the cooled light hydrocarbon stream 216 in a mixer 116 and the heavy fraction 206 may be fed into the separator 108 .
- the separator 108 separates the heavy fraction 206 into a bottom effluent stream 208 and a top effluent stream 214 .
- the bottom effluent stream 208 may be fed into a reboiler 110 , which may receive energy 302 by being heated, and separates the bottom effluent stream 208 into a recycle stream 210 and the heavy hydrocarbon stream 212 .
- the top effluent 214 may be fed into the compressor 112 that receives mechanical or electrical energy 304 and increases the pressure and/or temperature of the tope effluent 214 , thereby creating a compressed light hydrocarbon stream 216 .
- the compressed light hydrocarbon stream 216 may optionally be cooled, for example, by the heat exchanger 114 , which may be an air cooler, to produce a cooled light hydrocarbon stream 218 .
- the cooled light hydrocarbon stream 218 may then be mixed with the light fraction 220 in the mixer 116 .
- the resulting mixed light hydrocarbon stream 222 may then be processed as described above for the cooled light hydrocarbon stream 216 in FIG. 1 to produce the carbon dioxide-lean stream 234 .
- the hydrocarbon feed stream 200 may contain a mixture of hydrocarbons and carbon dioxide. Numerous types of hydrocarbons may be present in the hydrocarbon feed stream 200 , including methane, ethane, propane, i-butane, n-butane, i-pentane, n-pentane, hexane, octane, and other hydrocarbon compounds. For example, the hydrocarbon feed stream 200 may contain from about 10 percent to about 60 percent methane, no more than about 10 percent ethane, and no more than about 5 percent propane and heavier hydrocarbons (C 3+ ).
- the hydrocarbon feed stream 200 may contain any carbon dioxide concentration, in various embodiments the hydrocarbon feed stream 200 contains from about 10 percent to about 90 percent, from about 30 percent to about 80 percent, or from about 50 percent to about 70 percent of the carbon dioxide.
- the hydrocarbon feed stream 200 may also include other compounds such as water, nitrogen, hydrogen sulfide (H 2 S), and/or other acid gases.
- the hydrocarbon feed stream 200 may be in any state including a liquid state, a vapor state, or a combination of liquid and vapor states.
- the carbon dioxide-lean stream 234 may contain a mixture of hydrocarbons and carbon dioxide. Specifically, the composition of the carbon dioxide-lean stream 234 may contain an increased methane concentration and a decreased carbon dioxide concentration compared to the hydrocarbon feed stream 200 . In embodiments, the carbon dioxide-lean stream 234 contains less than about 60 percent, from about 20 percent to about 50 percent, or from about 30 percent to about 40 percent of the carbon dioxide. In yet other embodiments, the carbon dioxide concentration in the carbon dioxide-lean stream 234 is at least about 20 percent, at least about 40 percent, or at least about 60 percent less than the carbon dioxide concentration present in the hydrocarbon feed stream 200 .
- the carbon dioxide-lean stream 234 may also contain a reduced concentration of C3+ compared to the hydrocarbon feed stream 200 .
- the carbon dioxide-lean stream 234 comprises less than about 5 percent, less than about 1 percent, or is substantially free of C3+.
- the C3+ concentration in the carbon dioxide-lean stream 234 is at least about 20 percent, at least about 40 percent, or at least about 60 percent less than the C3+ concentration present in the hydrocarbon feed stream 200 .
- the carbon dioxide-lean stream 234 contains at least about 90 percent, at least about 98 percent, or at least about 99 percent of a combination of methane and carbon dioxide.
- the heavy hydrocarbon streams 212 , 254 may contain a mixture of heavy hydrocarbons and some other compounds. Specifically, the composition of the heavy hydrocarbon streams 212 , 254 contains an increased C3+ concentration and a decreased methane concentration, ethane, and carbon dioxide compared to the hydrocarbon feed stream 200 . In embodiments, the heavy hydrocarbon streams 212 , 254 comprises at least about 90 percent, at least about 95 percent, or at least about 99 percent C3+. In other embodiments, the heavy hydrocarbon streams 212 , 254 comprises less than about 5 percent, less than about 1 percent, or is substantially free of methane and/or ethane.
- the heavy hydrocarbon streams 212 , 254 contains less than about 10 percent, less than about 5 percent, or less than about 1 percent of the carbon dioxide.
- the heavy hydrocarbon streams 212 , 254 comprises at least about 20 percent, at least about 40 percent, or at least about 60 percent less carbon dioxide than the hydrocarbon feed stream 200 .
- the heavy hydrocarbon streams 212 , 254 described herein are suitable for use or sale as natural gas liquids (NGL).
- the carbon dioxide-rich stream 244 described herein may comprise a mixture of hydrocarbons and carbon dioxide. Specifically, the carbon dioxide-rich stream 244 contains a decreased concentration of hydrocarbons and an increased carbon dioxide concentration compared to the hydrocarbon feed stream 200 . In various embodiments, the carbon dioxide-rich stream 244 comprises less than about 10 percent, less than about 5 percent, or is substantially free of hydrocarbons. In other embodiments, the carbon dioxide-rich stream 244 contains at least about 80 percent, at least about 90 percent, or at least about 95 percent of the carbon dioxide.
- the carbon dioxide-rich stream 244 described herein may be vented, transported, sold, or used for other purposes including reinjection into a subterranean formation.
- the acid gas stream 250 described herein may comprise a mixture of hydrocarbons and at least one acid gas, such as H 2 S or carbon dioxide. Specifically, the composition of the acid gas stream 250 may contain a decreased hydrocarbon concentration and an increased acid gas concentration compared to the hydrocarbon feed stream 200 . In various embodiments, the acid gas stream 250 comprises less than about 10 percent, less than about 5 percent, or is substantially free of hydrocarbons. In other embodiments, the acid gas stream 250 contains at least about 90 percent, at least about 95 percent, or at least about 99 percent of the acid gas. The acid gas stream 250 described herein may be vented, sold, reinjected, or otherwise disposed of as desired.
- the hydrocarbon sweetening process 130 may be any sweetening process
- the hydrocarbon sweetening process 130 is a physical solvent process.
- the physical solvent process sweetens the hydrocarbon stream by using an organic solvent to absorb the carbon dioxide from the hydrocarbon stream.
- these physical solvents include SELEXOL®, RECTISOL®, PURISM®, and FLUOR® solvents such as propylene carbonate.
- the physical solvent process begins by contacting the carbon dioxide-lean stream 234 with the solvent at high pressure. The solvent absorbs the carbon dioxide such that subsequent separation of the solvent from the hydrocarbons produces a hydrocarbon stream with a relatively low carbon dioxide concentration.
- the carbon dioxide-loaded solvent is then regenerated by lowering the pressure of the solvent, typically through a series of flash drums, which causes the carbon dioxide to separate from the solvent.
- the solvent is then compressed and recycled into the hydrocarbon stream, while the carbon dioxide is vented or sold.
- the hydrocarbon sweetening process 130 may be a membrane separation process.
- Membrane separation processes use membranes to separate carbon dioxide from the carbon dioxide-lean stream 234 at the molecular level. Specifically, the pores in the membranes are sized to allow carbon dioxide to pass through the membrane and form a permeate gas, while the larger hydrocarbon molecules bypass the membrane and form a residue gas. Depending on the composition of the hydrocarbons, this configuration may be reversed such that the carbon dioxide forms the residue gas and the hydrocarbons form the permeate gas. Because the membrane process is dependent on, among other factors, the composition of the hydrocarbons, the selection of the pore size is best determined by persons of ordinary skill in the art.
- the hydrocarbon sweetening process 130 may be a carbon dioxide recovery process.
- a suitable carbon dioxide recovery process is the Ryan-Holmes process.
- the Ryan-Holmes process uses a solvent and a plurality of columns to separate the carbon dioxide-lean stream 234 into a carbon dioxide-rich stream, a methane-rich stream, and ethane-rich stream, and a heavy hydrocarbon stream.
- the columns may include a demethanizer, a carbon dioxide recovery unit, a propane recovery unit, and a solvent recovery unit.
- the columns are arranged in series with the solvent being recycled to the first column in the series. The specific arrangement of the various columns depends on the composition of the feed hydrocarbon stream and is best determined by persons of ordinary skill in the art.
- the hydrocarbon sweetening process 130 may be a process other than the exemplary processes described herein.
- the processing capacity of the hydrocarbon sweetening process 130 is increased.
- the processing capacity of the hydrocarbon sweetening process 130 may be directly proportional to the decrease in carbon dioxide concentration between the hydrocarbon feed stream 100 and the carbon dioxide-lean stream 234 .
- the processing capacity of the hydrocarbon sweetening process 130 may be directly proportional to the decrease in flow rate between the hydrocarbon feed stream 100 and the carbon dioxide-lean stream 234 .
- the processing capacity of the hydrocarbon sweetening process 130 is also doubled.
- the two affects may also be cumulative such that if the carbon dioxide concentration of the carbon dioxide-lean stream 234 is half of the carbon dioxide concentration of the hydrocarbon feed stream 100 and the flow rate of the carbon dioxide-lean stream 234 is half of the flow rate of the hydrocarbon feed stream 100 , then the processing capacity of the hydrocarbon sweetening process 130 is increased by a factor of four.
- the separators 106 , 108 , 120 , 134 may be any of a variety of process equipment suitable for separating a stream into two separate streams having different compositions, states, temperatures, and/or pressures.
- one or more of the separators 106 , 108 , 120 , 134 may be a column having trays, packing, or some other type of complex internal structure. Examples of such columns include scrubbers, strippers, absorbers, adsorbers, packed columns, and distillation columns having valve, sieve, or other types of trays. Such columns may employ weirs, downspouts, internal baffles, temperature, and/or pressure control elements.
- Such columns may also employ some combination of reflux condensers and/or reboilers, including intermediate stage condensers and reboilers.
- one or more of the separators 106 , 108 , 120 , 134 may be a phase separator.
- a phase separator is a vessel that separates an inlet stream into a substantially vapor stream and a substantially liquid stream, such as a knock-out drum or a flash drum.
- Such vessels may have some internal baffles, temperature, and/or pressure control elements, but generally lack any trays or other type of complex internal structure commonly found in columns.
- one or more of the separators 106 , 108 , 120 , 134 may be any other type of separator, such as a membrane separator.
- the reboilers 110 , 124 and condensers 122 , 132 described herein may be any of a variety of process equipment suitable for changing the temperature and/or separating any of the streams described herein.
- the reboilers 110 , 124 and the condensers 122 , 132 may be any vessel that separates an inlet stream into a substantially vapor stream and a substantially liquid stream. These vessels typically have some internal baffles, temperature, and/or pressure control elements, but generally lack any trays or other type of complex internal structure found in other vessels.
- heat exchangers and kettle-type reboilers may be used as the reboilers 110 , 124 and condensers 122 , 132 described herein.
- the heat exchangers 102 , 104 , 114 , 118 , 126 described herein may be any of a variety of process equipment suitable for heating or cooling any of the streams described herein.
- heat exchangers 102 , 104 , 114 , 118 , 126 are relatively simple devices that allow heat to be exchanged between two fluids without the fluids directly contacting each other.
- one of the fluids is atmospheric air, which may be forced over tubes or coils using one or more fans.
- the types of heat exchangers 102 , 104 , 114 , 118 , 126 suitable for use with the carbon dioxide fractionalization process 100 include shell and tube, kettle-type, air cooled, hairpin, bayonet, and plate-fin heat exchangers.
- the compressor 112 and pump 128 described herein may be any of a variety of process equipment suitable for increasing the pressure, temperature, and/or density of any of the streams described herein.
- compressors are associated with vapor streams and pumps are associated with liquid streams; however such a limitation should not be read into the present processes as the compressors and pumps described herein may be interchangeable based upon the specific conditions and compositions of the streams.
- the types of compressors and pumps suitable for the uses described herein include centrifugal, axial, positive displacement, rotary, and reciprocating compressors and pumps.
- the carbon dioxide fractionalization process 100 may contain additional compressors and/or pumps other than those described herein.
- the mixer 116 described herein may either be a dynamic mixer or a static mixer.
- Dynamic mixers are mixers that employ motion or mechanical agitation to mix two or more streams.
- a dynamic mixer may be a tank with a paddle operating either in a continuous or batch mode.
- static mixers are mixers that do not employ any motion or mechanical agitation to mix two or more streams.
- a static mixer may be a convergence of piping designed to combine two streams, such as a pipe tee. Either type of mixer may be configured with internal baffles to promote the mixing of the feed streams.
- the energy streams 300 , 302 , 304 , 306 , 308 , 310 , 312 , 314 described herein may be derived from any number of suitable sources.
- heat may be added to a process stream using steam, turbine exhaust, or some other hot fluid and a heat exchanger.
- heat may be removed from a process stream by using a refrigerant, air, or some other cold fluid and a heat exchanger.
- electrical energy can be supplied to compressors, pumps, and other mechanical equipment to increase the pressure or other physical properties of a fluid.
- turbines, generators, or other mechanical equipment can be used to extract physical energy from a stream and optionally convert the physical energy into electrical energy.
- the carbon dioxide fractionalization process 100 described herein has many advantages.
- One advantage is that it purifies a hydrocarbon stream used by one of the hydrocarbon sweetening processes 130 described above.
- the carbon dioxide fractionalization process 100 purities the hydrocarbon stream by removing some of the carbon dioxide and C3+ from the hydrocarbon stream.
- the purification of the hydrocarbon stream improves the performance of the hydrocarbon sweetening process 130 by reducing the carbon dioxide and C3+ loading on the hydrocarbon sweetening process 130 .
- the reduction in loading increases the processing capacity for the hydrocarbon sweetening process 130 , which is particularly advantageous for existing processing facilities.
- the addition of the carbon dioxide fractionalization process 100 to existing hydrocarbon sweetening processes 130 may reduce the energy requirements of the combined processes.
- the carbon dioxide fractionalization process 100 liquefies some of the carbon dioxide and C 3 in the hydrocarbon feed and feeds the carbon dioxide-lean stream 234 to the sweetening process 130 , thereby reducing the compression requirements within the hydrocarbon sweetening process 130 .
- the reduction in compression requirements may decrease the total energy requirements of the two processes per unit amount of hydrocarbons, e.g. Btu/SCF (British thermal units per standard cubic foot of gas).
- a process simulation was performed using the carbon dioxide fractionalization process 100 shown in FIG. 1 .
- the simulation was performed using the Hyproteeh Ltd. HYSYS Process v2.1.1 (Build 3198) software package.
- the carbon dioxide fractionalization process 100 separated a West Texas hydrocarbon feed containing about 63 percent carbon dioxide into a carbon dioxide-lean stream 234 containing about 43 percent carbon dioxide, a carbon dioxide-rich stream 244 containing about 95 percent carbon dioxide, an acid gas stream 250 containing about 100 percent carbon dioxide and trace amounts of other acid gases, and a heavy hydrocarbon stream containing about 99 percent C 3+ . It is notable that the process produces 454 gallons per minute of pipeline-grade liquefied carbon dioxide.
- the carbon dioxide produced by a SELEXOL® plant without this process produces a similar amount of gaseous carbon dioxide, but at atmospheric pressure or at a vacuum.
- the compression requirements for such a gaseous carbon dioxide stream are large, e.g. 25,000 BTU per thousand standard cubic feet (MSCF), and are generally cost prohibitive.
- MSCF standard cubic feet
- the material streams, their compositions, and the associated energy streams produced by the simulation are provided in tables 1, 2, and 3 below. The specified values are indicated by an asterisk (*).
- the physical properties are provided in degrees Fahrenheit (F), pounds per square inch gauge (psig), million standard cubic feet per day (MMSCFD), pounds per hour (lb/hr), U.S. gallons per minute (USGPM), and British thermal units per hour (Btu/hr).
- a process simulation was performed using the carbon dioxide fractionalization process 100 shown in FIG. 2 .
- the simulation was performed using the Hyprotech Ltd. HYSYS Process v2.1.1 (Build 3198) software package.
- the carbon dioxide fractionalization process 100 separated a West Texas hydrocarbon feed containing about 63 percent carbon dioxide into a carbon dioxide-lean stream 234 containing about 36 percent carbon dioxide, a carbon dioxide-rich stream 244 containing about 95 percent carbon dioxide, and a heavy hydrocarbon stream containing about 93 percent C3+.
- the material streams, their compositions, and the associated energy streams produced by the simulation are provided in tables 4, 5, and 6 below.
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Abstract
A process comprising receiving a hydrocarbon feed stream comprising carbon dioxide, separating the hydrocarbon feed stream into a light hydrocarbon stream and a heavy hydrocarbon stream, separating the light hydrocarbon stream into a carbon dioxide-rich stream and a carbon dioxide-lean stream, and feeding the carbon dioxide-lean stream into a hydrocarbon sweetening process, thereby increasing the processing capacity of the hydrocarbon sweetening process compared to the processing capacity of the hydrocarbon sweetening process when fed the hydrocarbon feed stream. Included is an apparatus comprising a first separation unit that receives a hydrocarbon feed stream containing carbon dioxide and produces a heavy hydrocarbon stream and a light hydrocarbon stream, and a second separation unit that receives the light hydrocarbon stream and produces a carbon dioxide-rich stream and a carbon dioxide-lean stream, wherein the apparatus is configured to feed the carbon dioxide-lean stream to a physical solvent, membrane, or carbon dioxide recovery process.
Description
- This application is a continuation of U.S. patent application Ser. No. 12/824,382, filed Jun. 28, 2010, which is a divisional of U.S. patent application Ser. No. 11/621,913 filed Jan. 10, 2007, now U.S. Pat. No. 7,777,088, the contents of which are incorporated herein by reference.
- Not applicable.
- Not applicable.
- Carbon dioxide is a naturally occurring substance in most hydrocarbon formations. While the carbon dioxide concentration will depend on the location of the formation, carbon dioxide concentrations as high as eighty percent are common in many areas, such as West Texas. Moreover, the implementation of tertiary recovery operations, such as carbon-dioxide injection into the subterranean wellbore, can increase the carbon dioxide concentration within the produced hydrocarbons. In either case, the carbon dioxide concentration of the produced hydrocarbons may be sufficiently high to require the carbon dioxide concentration to be reduced before the hydrocarbons can be refined or further processed.
- Several solutions are known for reducing the carbon dioxide concentration or “sweetening” a hydrocarbon stream. For example, amine processes, physical solvent processes, membrane processes, and carbon dioxide recovery processes have all been used to sweeten hydrocarbon streams. The processing facilities employing these hydrocarbon sweetening processes are generally sized for a specific processing capacity and hydrocarbon feed stream composition. As such, when the carbon dioxide concentration of the hydrocarbon feed stream increases or additional feedstock comes online, then an additional processing facility must be constructed to compensate for the change in hydrocarbon feed stream composition or the increased feedstock. The construction of a new processing facility is undesirable because of the substantial capital cost, operating costs, and time delay inherent in such a solution.
- In one aspect, the disclosure includes a process comprising receiving a hydrocarbon feed stream comprising carbon dioxide, separating the hydrocarbon feed stream into a light hydrocarbon stream and a heavy hydrocarbon stream, separating the light hydrocarbon stream into a carbon dioxide-rich stream and a carbon dioxide-lean stream, and feeding the carbon dioxide-lean stream into a hydrocarbon sweetening process, thereby increasing the processing capacity of the hydrocarbon sweetening process compared to the processing capacity of the hydrocarbon sweetening process when fed the hydrocarbon feed stream.
- In another aspect, the disclosure includes an apparatus comprising a first separation unit that receives a hydrocarbon feed stream containing carbon dioxide and produces a heavy hydrocarbon stream and a light hydrocarbon stream, and a second separation unit that receives the light hydrocarbon stream and produces a carbon dioxide-rich stream and a carbon dioxide-lean stream, wherein the apparatus is configured to feed the carbon dioxide-lean stream to a physical solvent process, a membrane process, a chemical solvent process, an extractive distillation process or a carbon dioxide recovery process.
- In a third aspect, the disclosure includes a process comprising receiving a hydrocarbon feed stream comprising carbon dioxide, cooling the hydrocarbon feed stream using a carbon dioxide-lean stream, separating the cooled hydrocarbon feed stream into a light hydrocarbon stream and a heavy hydrocarbon stream, compressing the light hydrocarbon stream, cooling the compressed light hydrocarbon stream using the carbon dioxide-lean stream, separating the compressed light hydrocarbon stream into a carbon dioxide-rich stream and the carbon dioxide-lean stream, and removing at least some of the carbon dioxide in the carbon dioxide-lean stream using a hydrocarbon sweetening process.
-
FIG. 1 is a process flow diagram of one embodiment of the carbon dioxide fractionalization process; and -
FIG. 2 is a process flow diagram of another embodiment of the carbon dioxide fractionalization process. - Disclosed herein is a carbon dioxide fractionalization process that may be positioned in front of an existing hydrocarbon sweetening process to increase the processing capacity of the hydrocarbon sweetening process. Specifically, the carbon dioxide fractionalization process purifies the hydrocarbon feed stream by removing at least some of the carbon dioxide and the heavy hydrocarbons from a hydrocarbon feed stream. The purification of the hydrocarbon stream reduces the carbon dioxide and heavy hydrocarbon loading on the hydrocarbon sweetening process, thereby increasing the processing capacity of the hydrocarbon sweetening process. Furthermore, the carbon dioxide fractionalization process produces a carbon dioxide-rich stream that may be injected into a subterranean formation.
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FIG. 1 illustrates one embodiment of the carbondioxide fractionalization process 100. The carbondioxide fractionalization process 100 separates a feed mixture comprising ahydrocarbon feed stream 200 into aheavy hydrocarbon stream 254, anacid gas stream 250, a carbon dioxide-rich stream 244, and a carbon dioxide-lean stream 234, the compositions of which are discussed in detail below. The carbondioxide fractionalization process 100 receives thehydrocarbon feed stream 200 and may pass thehydrocarbon feed stream 200 through aheat exchanger 102 that uses the cooled carbon dioxide-lean stream 232 to reduce the temperature of thehydrocarbon feed stream 200. Afirst separation unit 101 that comprises one or more of aseparator 108, areboiler 110, acondenser 132, and aseparator 134 may then remove the heavy hydrocarbons from the cooledhydrocarbon feed stream 202. Specifically, theseparator 108 separates the cooledhydrocarbon feed stream 202 into a bottomeffluent stream 208 and atop effluent stream 214. Thetop effluent stream 214 may then be fed into acondenser 132, which may give offenergy 312 by being cooled, and separates thetop effluent stream 214 into areflux stream 246 and alight hydrocarbon stream 248. Similarly, the bottomeffluent stream 208 may be fed into thereboiler 110, which may receiveenergy 302 by being, heated, and separates thebottom effluent stream 208 into arecycle stream 210 and aheavy hydrocarbon stream 212. Theheavy hydrocarbon stream 212 may then be fed into aseparator 134 that separates anacid gas stream 250 from theheavy hydrocarbon stream 252. Theheavy hydrocarbon stream 252 may optionally be cooled by aheat exchanger 114, for example an air cooler, to produce theheavy hydrocarbon stream 254. - Returning to the
light hydrocarbon stream 248, thelight hydrocarbon stream 248 may be fed into acompressor 112 that receives mechanical orelectrical energy 304 and increases the pressure and/or temperature of thelight hydrocarbon stream 248, thereby creating a compressedlight hydrocarbon stream 216. The compressedlight hydrocarbon stream 216 may then be fed into aheat exchanger 118 that uses a chilled carbon dioxide-lean stream 230 to reduce the temperature of the cooledlight hydrocarbon stream 216, thereby producing a chilledlight hydrocarbon stream 224. Asecond separation unit 103 that comprises one or more of aseparator 120, areboiler 124, and acondenser 122 may then remove at least some of the carbon dioxide from the chilledlight hydrocarbon stream 224. Theseparator 120 forms a first effluent leaner in carbon dioxide than the feed mixture and a second effluent richer in carbon dioxide than the feed mixture. Specifically, theseparator 120 separates the chilledlight hydrocarbon stream 224 into aheavy effluent stream 236 and alight effluent stream 226. Thelight effluent stream 226 may be fed into thecondenser 122, which may give offenergy 306 by being cooled, and separates thelight effluent stream 226 into a condensed portion, orreflux stream 228 and the chilled carbon dioxide-lean stream 230. The chilled carbon dioxide-lean stream 230 may then be passed through theheat exchangers hydrocarbon sweetening process 130. Thehydrocarbon sweetening process 130 may be any process that removes carbon dioxide from a hydrocarbon stream to make the hydrocarbon stream suitable for transportation and/or further processing. Persons of ordinary skill in the art are aware of numerous differenthydrocarbon sweetening processes 130, as illustrated by Field Processing of Petroleum, Vol. 1: Natural Gas by Manning et al., incorporated herein by reference as if reproduced in its entirety. Several examples of thehydrocarbon sweetening process 130 are discussed in detail below. - Returning to the
separator 120, theheavy effluent stream 236 may be fed into thereboiler 124, which may receiveenergy 308 in the form of heat, and separates theheavy effluent stream 236 into arecycle stream 238 and a cooled carbon dioxide-rich stream 240. The cooled carbon dioxide-rich stream 240 may optionally be combined with theacid gas stream 250, if desired. The cooled carbon dioxide-rich stream 240 may then be fed through aheat exchanger 126 that further cools the cooled carbon dioxide-rich stream 240 by removingenergy 310 from the cooled carbon dioxide-rich stream 240, thereby producing the chilled carbon dioxide-rich stream 242. The chilled carbon dioxide-rich stream 242 may also be fed to apump 128 that usesenergy 314 to pump the carbon dioxide-rich stream 244 to another location, perhaps for injection into a subterranean formation. -
FIG. 2 illustrates another embodiment of the carbondioxide fractionalization process 100. Similar to the embodiment shown inFIG. 1 , the carbondioxide fractionalization process 100 shown inFIG. 2 separates thehydrocarbon feed stream 200 into theheavy hydrocarbon stream 212, the carbon dioxide-rich stream 244, and the carbon dioxide-lean stream 234, the compositions of which are discussed in detail below. The carbondioxide fractionalization process 100 receives thehydrocarbon feed stream 200 and passes thehydrocarbon feed stream 200 through aheat exchanger 102 that uses the cooled carbon dioxide-lean stream 232 to reduce the temperature of thehydrocarbon feed stream 200. After the cooledhydrocarbon feed stream 202 exits theheat exchanger 102, the hydrocarbon feed stream is fed into theoptional heat exchanger 104, which further cools the cooledhydrocarbon feed stream 202 by removing some of itsenergy 300, thereby producing a chilledhydrocarbon feed stream 202. - A
first separation unit 101 that comprises one or more ofseparators reboiler 110 may then remove the heavy hydrocarbons from the cooled chilledhydrocarbon feed stream 202. Specifically, the chilledhydrocarbon feed stream 202 may be fed into aseparator 106 that separates the chilledhydrocarbon feed stream 202 into alight fraction 220 and aheavy fraction 206. In an embodiment, thelight fraction 220 may be a vapor phase and theheavy fraction 206 may be a liquid phase. Thelight fraction 220 may be combined with the cooledlight hydrocarbon stream 216 in amixer 116 and theheavy fraction 206 may be fed into theseparator 108. Theseparator 108 separates theheavy fraction 206 into a bottomeffluent stream 208 and atop effluent stream 214. The bottomeffluent stream 208 may be fed into areboiler 110, which may receiveenergy 302 by being heated, and separates thebottom effluent stream 208 into arecycle stream 210 and theheavy hydrocarbon stream 212. Thetop effluent 214 may be fed into thecompressor 112 that receives mechanical orelectrical energy 304 and increases the pressure and/or temperature of thetope effluent 214, thereby creating a compressedlight hydrocarbon stream 216. The compressedlight hydrocarbon stream 216 may optionally be cooled, for example, by theheat exchanger 114, which may be an air cooler, to produce a cooledlight hydrocarbon stream 218. The cooledlight hydrocarbon stream 218 may then be mixed with thelight fraction 220 in themixer 116. The resulting mixedlight hydrocarbon stream 222 may then be processed as described above for the cooledlight hydrocarbon stream 216 inFIG. 1 to produce the carbon dioxide-lean stream 234. - The
hydrocarbon feed stream 200 may contain a mixture of hydrocarbons and carbon dioxide. Numerous types of hydrocarbons may be present in thehydrocarbon feed stream 200, including methane, ethane, propane, i-butane, n-butane, i-pentane, n-pentane, hexane, octane, and other hydrocarbon compounds. For example, thehydrocarbon feed stream 200 may contain from about 10 percent to about 60 percent methane, no more than about 10 percent ethane, and no more than about 5 percent propane and heavier hydrocarbons (C3+). Although thehydrocarbon feed stream 200 may contain any carbon dioxide concentration, in various embodiments thehydrocarbon feed stream 200 contains from about 10 percent to about 90 percent, from about 30 percent to about 80 percent, or from about 50 percent to about 70 percent of the carbon dioxide. Thehydrocarbon feed stream 200 may also include other compounds such as water, nitrogen, hydrogen sulfide (H2S), and/or other acid gases. Finally, thehydrocarbon feed stream 200 may be in any state including a liquid state, a vapor state, or a combination of liquid and vapor states. Finally, unless otherwise stated, the percentages herein are provided on a mole basis. - Similar to the
hydrocarbon feed stream 200, the carbon dioxide-lean stream 234 may contain a mixture of hydrocarbons and carbon dioxide. Specifically, the composition of the carbon dioxide-lean stream 234 may contain an increased methane concentration and a decreased carbon dioxide concentration compared to thehydrocarbon feed stream 200. In embodiments, the carbon dioxide-lean stream 234 contains less than about 60 percent, from about 20 percent to about 50 percent, or from about 30 percent to about 40 percent of the carbon dioxide. In yet other embodiments, the carbon dioxide concentration in the carbon dioxide-lean stream 234 is at least about 20 percent, at least about 40 percent, or at least about 60 percent less than the carbon dioxide concentration present in thehydrocarbon feed stream 200. The carbon dioxide-lean stream 234 may also contain a reduced concentration of C3+ compared to thehydrocarbon feed stream 200. In various embodiments, the carbon dioxide-lean stream 234 comprises less than about 5 percent, less than about 1 percent, or is substantially free of C3+. In yet other embodiments, the C3+ concentration in the carbon dioxide-lean stream 234 is at least about 20 percent, at least about 40 percent, or at least about 60 percent less than the C3+ concentration present in thehydrocarbon feed stream 200. Finally, in other embodiments, the carbon dioxide-lean stream 234 contains at least about 90 percent, at least about 98 percent, or at least about 99 percent of a combination of methane and carbon dioxide. - The
heavy hydrocarbon streams heavy hydrocarbon streams hydrocarbon feed stream 200. In embodiments, theheavy hydrocarbon streams heavy hydrocarbon streams heavy hydrocarbon streams heavy hydrocarbon streams hydrocarbon feed stream 200. In an embodiment, theheavy hydrocarbon streams - The carbon dioxide-
rich stream 244 described herein may comprise a mixture of hydrocarbons and carbon dioxide. Specifically, the carbon dioxide-rich stream 244 contains a decreased concentration of hydrocarbons and an increased carbon dioxide concentration compared to thehydrocarbon feed stream 200. In various embodiments, the carbon dioxide-rich stream 244 comprises less than about 10 percent, less than about 5 percent, or is substantially free of hydrocarbons. In other embodiments, the carbon dioxide-rich stream 244 contains at least about 80 percent, at least about 90 percent, or at least about 95 percent of the carbon dioxide. The carbon dioxide-rich stream 244 described herein may be vented, transported, sold, or used for other purposes including reinjection into a subterranean formation. - The
acid gas stream 250 described herein may comprise a mixture of hydrocarbons and at least one acid gas, such as H2S or carbon dioxide. Specifically, the composition of theacid gas stream 250 may contain a decreased hydrocarbon concentration and an increased acid gas concentration compared to thehydrocarbon feed stream 200. In various embodiments, theacid gas stream 250 comprises less than about 10 percent, less than about 5 percent, or is substantially free of hydrocarbons. In other embodiments, theacid gas stream 250 contains at least about 90 percent, at least about 95 percent, or at least about 99 percent of the acid gas. Theacid gas stream 250 described herein may be vented, sold, reinjected, or otherwise disposed of as desired. - Although the
hydrocarbon sweetening process 130 may be any sweetening process, in one embodiment thehydrocarbon sweetening process 130 is a physical solvent process. The physical solvent process sweetens the hydrocarbon stream by using an organic solvent to absorb the carbon dioxide from the hydrocarbon stream. Examples of these physical solvents include SELEXOL®, RECTISOL®, PURISM®, and FLUOR® solvents such as propylene carbonate. The physical solvent process begins by contacting the carbon dioxide-lean stream 234 with the solvent at high pressure. The solvent absorbs the carbon dioxide such that subsequent separation of the solvent from the hydrocarbons produces a hydrocarbon stream with a relatively low carbon dioxide concentration. The carbon dioxide-loaded solvent is then regenerated by lowering the pressure of the solvent, typically through a series of flash drums, which causes the carbon dioxide to separate from the solvent. The solvent is then compressed and recycled into the hydrocarbon stream, while the carbon dioxide is vented or sold. - Alternatively, the
hydrocarbon sweetening process 130 may be a membrane separation process. Membrane separation processes use membranes to separate carbon dioxide from the carbon dioxide-lean stream 234 at the molecular level. Specifically, the pores in the membranes are sized to allow carbon dioxide to pass through the membrane and form a permeate gas, while the larger hydrocarbon molecules bypass the membrane and form a residue gas. Depending on the composition of the hydrocarbons, this configuration may be reversed such that the carbon dioxide forms the residue gas and the hydrocarbons form the permeate gas. Because the membrane process is dependent on, among other factors, the composition of the hydrocarbons, the selection of the pore size is best determined by persons of ordinary skill in the art. - In yet another embodiment, the
hydrocarbon sweetening process 130 may be a carbon dioxide recovery process. One example of a suitable carbon dioxide recovery process is the Ryan-Holmes process. The Ryan-Holmes process uses a solvent and a plurality of columns to separate the carbon dioxide-lean stream 234 into a carbon dioxide-rich stream, a methane-rich stream, and ethane-rich stream, and a heavy hydrocarbon stream. The columns may include a demethanizer, a carbon dioxide recovery unit, a propane recovery unit, and a solvent recovery unit. The columns are arranged in series with the solvent being recycled to the first column in the series. The specific arrangement of the various columns depends on the composition of the feed hydrocarbon stream and is best determined by persons of ordinary skill in the art. Finally, persons of ordinary skill in the art will appreciate that thehydrocarbon sweetening process 130 may be a process other than the exemplary processes described herein. - When the carbon
dioxide fractionalization process 100 is implemented prior to ahydrocarbon sweetening process 130, the processing capacity of thehydrocarbon sweetening process 130 is increased. Specifically, the processing capacity of thehydrocarbon sweetening process 130 may be directly proportional to the decrease in carbon dioxide concentration between thehydrocarbon feed stream 100 and the carbon dioxide-lean stream 234. For example, if the carbon dioxide concentration of the carbon dioxide-lean stream 234 is half of the carbon dioxide concentration of thehydrocarbon feed stream 100, then the processing capacity of thehydrocarbon sweetening process 130 is doubled. In addition, the processing capacity of thehydrocarbon sweetening process 130 may be directly proportional to the decrease in flow rate between thehydrocarbon feed stream 100 and the carbon dioxide-lean stream 234. For example, if the flow rate of the carbon dioxide-lean stream 234 is half of the flow rate of thehydrocarbon feed stream 100, then the processing capacity of thehydrocarbon sweetening process 130 is also doubled. The two affects may also be cumulative such that if the carbon dioxide concentration of the carbon dioxide-lean stream 234 is half of the carbon dioxide concentration of thehydrocarbon feed stream 100 and the flow rate of the carbon dioxide-lean stream 234 is half of the flow rate of thehydrocarbon feed stream 100, then the processing capacity of thehydrocarbon sweetening process 130 is increased by a factor of four. - The
separators separators separators separators - The
reboilers condensers reboilers condensers reboilers condensers - The
heat exchangers heat exchangers heat exchangers dioxide fractionalization process 100 include shell and tube, kettle-type, air cooled, hairpin, bayonet, and plate-fin heat exchangers. - The
compressor 112 and pump 128 described herein may be any of a variety of process equipment suitable for increasing the pressure, temperature, and/or density of any of the streams described herein. Generally, compressors are associated with vapor streams and pumps are associated with liquid streams; however such a limitation should not be read into the present processes as the compressors and pumps described herein may be interchangeable based upon the specific conditions and compositions of the streams. The types of compressors and pumps suitable for the uses described herein include centrifugal, axial, positive displacement, rotary, and reciprocating compressors and pumps. Finally, the carbondioxide fractionalization process 100 may contain additional compressors and/or pumps other than those described herein. - The
mixer 116 described herein may either be a dynamic mixer or a static mixer. Dynamic mixers are mixers that employ motion or mechanical agitation to mix two or more streams. For example, a dynamic mixer may be a tank with a paddle operating either in a continuous or batch mode. In contrast, static mixers are mixers that do not employ any motion or mechanical agitation to mix two or more streams. For example, a static mixer may be a convergence of piping designed to combine two streams, such as a pipe tee. Either type of mixer may be configured with internal baffles to promote the mixing of the feed streams. - The energy streams 300, 302, 304, 306, 308, 310, 312, 314 described herein may be derived from any number of suitable sources. For example, heat may be added to a process stream using steam, turbine exhaust, or some other hot fluid and a heat exchanger. Similarly, heat may be removed from a process stream by using a refrigerant, air, or some other cold fluid and a heat exchanger. Further, electrical energy can be supplied to compressors, pumps, and other mechanical equipment to increase the pressure or other physical properties of a fluid. Similarly, turbines, generators, or other mechanical equipment can be used to extract physical energy from a stream and optionally convert the physical energy into electrical energy. Persons of ordinary skill in the art are aware of how to configure the processes described herein with the required
energy streams dioxide fractionalization process 100 may contain additional equipment, process steams, and/or energy streams other than those described herein. - The carbon
dioxide fractionalization process 100 described herein has many advantages. One advantage is that it purifies a hydrocarbon stream used by one of the hydrocarbon sweetening processes 130 described above. Specifically, the carbondioxide fractionalization process 100 purities the hydrocarbon stream by removing some of the carbon dioxide and C3+ from the hydrocarbon stream. The purification of the hydrocarbon stream improves the performance of thehydrocarbon sweetening process 130 by reducing the carbon dioxide and C3+ loading on thehydrocarbon sweetening process 130. The reduction in loading increases the processing capacity for thehydrocarbon sweetening process 130, which is particularly advantageous for existing processing facilities. Moreover, the addition of the carbondioxide fractionalization process 100 to existing hydrocarbon sweetening processes 130 may reduce the energy requirements of the combined processes. Specifically, the carbondioxide fractionalization process 100 liquefies some of the carbon dioxide and C3 in the hydrocarbon feed and feeds the carbon dioxide-lean stream 234 to thesweetening process 130, thereby reducing the compression requirements within thehydrocarbon sweetening process 130. The reduction in compression requirements may decrease the total energy requirements of the two processes per unit amount of hydrocarbons, e.g. Btu/SCF (British thermal units per standard cubic foot of gas). Other advantages will be apparent to persons of ordinary skill in the art. - In one example, a process simulation was performed using the carbon
dioxide fractionalization process 100 shown inFIG. 1 . The simulation was performed using the Hyproteeh Ltd. HYSYS Process v2.1.1 (Build 3198) software package. The carbondioxide fractionalization process 100 separated a West Texas hydrocarbon feed containing about 63 percent carbon dioxide into a carbon dioxide-lean stream 234 containing about 43 percent carbon dioxide, a carbon dioxide-rich stream 244 containing about 95 percent carbon dioxide, anacid gas stream 250 containing about 100 percent carbon dioxide and trace amounts of other acid gases, and a heavy hydrocarbon stream containing about 99 percent C3+. It is notable that the process produces 454 gallons per minute of pipeline-grade liquefied carbon dioxide. The carbon dioxide produced by a SELEXOL® plant without this process produces a similar amount of gaseous carbon dioxide, but at atmospheric pressure or at a vacuum. The compression requirements for such a gaseous carbon dioxide stream are large, e.g. 25,000 BTU per thousand standard cubic feet (MSCF), and are generally cost prohibitive. Thus, the present process allows carbon dioxide to be economically recovered and reused, unlike the prior processes. The material streams, their compositions, and the associated energy streams produced by the simulation are provided in tables 1, 2, and 3 below. The specified values are indicated by an asterisk (*). The physical properties are provided in degrees Fahrenheit (F), pounds per square inch gauge (psig), million standard cubic feet per day (MMSCFD), pounds per hour (lb/hr), U.S. gallons per minute (USGPM), and British thermal units per hour (Btu/hr). -
TABLE 1 Material Streams Name 200 248 202 224 Vapor Fraction 1.0000 1.0000 1.0000 1.0000 Temperature (F.) 100.0* −15.92 99.00* 60.00* Pressure (psig) 485.3* 385.3 480.3 980.3 Molar Flow (MMSCFD) 100.0* 99.82 100.0 99.82 Mass Flow (lb/hr) 3.731e+05 3.713e+05 3.731e+05 3.713e+05 Liquid Volume Flow 1176 1171 1176 1171 Heat Flow (Btu/hr) −1.305e+09 −1.316e+09 −1.305e+09 −1.315e+09 Name 230 240 232 234 Vapor Fraction 1.0000 0.0000 1.0000 1.0000 Temperature (F.) −5.769 65.16 92.33 92.78 Pressure (psig) 925.3 935.3 920.3 915.3 Molar Flow (MMSCFD) 61.13 38.68 61.13 61.13 Mass Flow (lb/hr) 1.896e+05 1.817e+05 1.896e+05 1.896e+05 Liquid Volume Flow 716.7 454.5 716.7 716.7 Heat Flow (Btu/hr) −6.242e+08 −7.078e+08 −6.145e+08 −6.145e+08 Name 244 242 218 212 Vapor Fraction 0.0000 0.0000 1.0000 0.0000 Temperature (F.) 72.39 55.00 123.3 264.0 Pressure (psig) 1785* 930.3 985.3* 395.3 Molar Flow (MMSCFD) 38.68 38.68 99.82 0.1832 Mass Flow (lb/hr) 1.817e+05 1.817e+05 3.713e+05 1801 Liquid Volume Flow 454.5 454.5 1171 5.233 Heat Flow (Btu/hr) −7.092e+08 −7.100e+08 1.306e+09 −1.905e+06 Name 250 252 254 Vapor Fraction 1.0000 0.0000 0.0000 Temperature (F.) 100.0* 265.2* 120.0* Pressure (psig) 485.3* 485.3* 465.3* Molar Flow (MMSCFD) 0.02473 0.1585 0.1585 Mass Flow (lb/hr) 119.5 1682 1682 Liquid Volume Flow (USGPM) 0.2892 4.944 4.944 Heat Flow (Btu/hr) −4.610e+05 −1.444e+06 −1.593e+06 -
TABLE 2 Stream Compositions Name 200 248 202 224 Comp Mole Frac 0.0000* 0.0000 0.0000 0.0000 (H2S) Comp Mole Frac 0.0051* 0.0051 0.0051 0.0051 (Nitrogen) Comp Mole Frac 0.6308* 0.6317 0.6308 0.6317 (CO2) Comp Mole Frac 0.3570* 0.3577 0.3570 0.3577 (Methane) Comp Mole Frac 0.0037* 0.0037 0.0037 0.0037 (Ethane) Comp Mole Frac 0.0013* 0.0013 0.0013 0.0013 (Propane) Comp Mole Frac 0.0002* 0.0002 0.0002 0.0002 (i-Butane) Comp Mole Frac 0.0005* 0.0004 0.0005 0.0004 (n-Butane) Comp Mole Frac 0.0000* 0.0000 0.0000 0.0000 (i-Pentane) Comp Mole Frac 0.0000* 0.0000 0.0000 0.0000 (n-Pentane) Comp Mole Frac 0.0007* 0.0000 0.0007 0.0000 (n-Hexane) Comp Mole Frac 0.0008* 0.0000 0.0008 0.0000 (n-Octane) Comp Mole Frac 0.0000* 0.0000 0.0000 0.0000 (H2O) Name 230 240 232 234 Comp Mole Frac 0.0000 0.0000 0.0000 0.0000 (H2S) Comp Mole Frac 0.0083 0.0001 0.0083 0.0083 (Nitrogen) Comp Mole Frac 0.4303 0.9500 0.4303 0.4303 (CO2) Comp Mole Frac 0.5568 0.0430 0.5568 0.5568 (Methane) Comp Mole Frac 0.0041 0.0031 0.0041 0.0041 (Ethane) Comp Mole Frac 0.0005 0.0025 0.0005 0.0005 (Propane) Comp Mole Frac 0.0000 0.0004 0.0000 0.0000 (i-Butane) Comp Mole Frac 0.0000 0.0010 0.0000 0.0000 (n-Butane) Comp Mole Frac 0.0000 0.0000 0.0000 0.0000 (i-Pentane) Comp Mole Frac 0.0000 0.0000 0.0000 0.0000 (n-Pentane) Comp Mole Frac 0.0000 0.0000 0.0000 0.0000 (n-Hexane) Comp Mole Frac 0.0000 0.0000 0.0000 0.0000 (n-Octane) Comp Mole Frac 0.0000 0.0000 0.0000 0.0000 (H2O) Name 244 242 218 212 Comp Mole Frac 0.0000 0.0000 0.0000 0.0000 (H2S) Comp Mole Frac 0.0001 0.0001 0.0051 0.0000 (Nitrogen) Comp Mole Frac 0.9500 0.9500 0.6317 0.1350 (CO2) Comp Mole Frac 0.0430 0.0430 0.3577 0.0001 (Methane) Comp Mole Frac 0.0031 0.0031 0.0037 0.0050 (Ethane) Comp Mole Frac 0.0025 0.0025 0.0013 0.0142 (Propane) Comp Mole Frac 0.0004 0.0004 0.0002 0.0078 (i-Butane) Comp Mole Frac 0.0010 0.0010 0.0004 0.0472 (n-Butane) Comp Mole Frac 0.0000 0.0000 0.0000 0.0000 (i-Pentane) Comp Mole Frac 0.0000 0.0000 0.0000 0.0000 (n-Pentane) Comp Mole Frac 0.0000 0.0000 0.0000 0.3813 (n-Hexane) Comp Mole Frac 0.0000 0.0000 0.0000 0.4094 (n-Octane) Comp Mole Frac 0.0000 0.0000 0.0000 0.0000 (H2O) Name 250 252 254 Comp Mole Frac (H2S) 0.0000 0.0000 0.0000 Comp Mole Frac (Nitrogen) 0.0000 0.0000 0.0000 Comp Mole Frac (CO2) 1.0000 0.0000 0.0000 Comp Mole Frac (Methane) 0.0000 0.0001 0.0001 Comp Mole Frac (Ethane) 0.0000 0.0058 0.0058 Comp Mole Frac (Propane) 0.0000 0.0164 0.0164 Comp Mole Frac (i-Butane) 0.0000 0.0090 0.0090 Comp Mole Frac (n-Butane) 0.0000 0.0545 0.0545 Comp Mole Frac (i-Pentane) 0.0000 0.0000 0.0000 Comp Mole Frac (n-Pentane) 0.0000 0.0000 0.0000 Comp Mole Frac (n-Hexane) 0.0000 0.4408 0.4408 Comp Mole Frac (n-Octane) 0.0000 0.4733 0.4733 Comp Mole Frac (H2O) 0.0000 0.0000 0.0000 -
TABLE 3 Energy Streams Name HeatFlow (Btu/hr) 308 8.518e+06 302 3.623e+05 304 1.027e+07 306 2.505e+07 314 7.719e+05 310 2.184e+06 312 1.293e+07 - In another example, a process simulation was performed using the carbon
dioxide fractionalization process 100 shown inFIG. 2 . The simulation was performed using the Hyprotech Ltd. HYSYS Process v2.1.1 (Build 3198) software package. The carbondioxide fractionalization process 100 separated a West Texas hydrocarbon feed containing about 63 percent carbon dioxide into a carbon dioxide-lean stream 234 containing about 36 percent carbon dioxide, a carbon dioxide-rich stream 244 containing about 95 percent carbon dioxide, and a heavy hydrocarbon stream containing about 93 percent C3+. The material streams, their compositions, and the associated energy streams produced by the simulation are provided in tables 4, 5, and 6 below. -
TABLE 4 Material Streams Name 200 204 206 222 Vapor Fraction 1.0000 0.8205 0.0000 1.0000 Temperature (F.) 100.0* 22.00* 22.00 34.23 Pressure (psig) 945.3* 935.3 935.3 935.3 Molar Flow (MMSCFD) 300.0* 300.0 53.85 299.6 Mass Flow (lb/hr) 1.119e+06 1.119e+06 2.343e+05 1.115e+06 Liquid Volume Flow 3529 3529 640.1 3516 Heat Flow (Btu/hr) −3.932e+09 −3.988e+09 −8.836e+08 −3.961e+09 Name 214 212 202 218 Vapor Fraction 1.0000 0.0000 1.0000 1.0000 Temperature (F.) −5.027 335.1 47.95 100.0* Pressure (psig) 335.3 340.3 940.3 960.3* Molar Flow (MMSCFD) 53.41 0.4397 300.0 53.41 Mass Flow (lb/hr) 2.299e+05 4409 1.119e+06 2.299e+05 Liquid Volume Flow 627.1 12.95 3529 627.1 (USGPM) Heat Flow (Btu/hr) −8.582e+08 −4.030e+06 −3.957e+09 −8.564e+08 Name 224 230 240 232 Vapor Fraction 1.0000 1.0000 0.00000 1.0000 Temperature (F.) 32.00* −20.00 61.65 −17.19 Pressure (psig) 930.3 895.3 900.3 890.3 Molar Flow (MMSCFD) 299.6 161.3 138.3 161.3 Mass Flow (lb/hr) 1.115e+06 4.649e+05 6.501e+05 4.649e+05 Liquid Volume Flow 3516 1890 1626 1890 (USGPM) Heat Flow (Btu/hr) −3.962e+09 −1.473e+09 −2.533e+09 −1.472e+09 Name 234 244 242 220 216 Vapor Fraction 1.0000 0.0000 0.0000 1.0000 1.0000 Temperature (F.) 85.00* 73.48 55.00* 22.00 155.2 Pressure (psig) 885.3 1785* 895.3 935.3 965.3 Molar Flow (MMSCFD) 161.3 138.3 138.3 246.2 53.41 Mass Flow (lb/hr) 4.649e+05 6.501e+05 6.501e+05 8.851e+05 2.299e+05 Liquid Volume Flow 1890 1626 1626 2889 627.1 (USGPM) Heat Flow (Btu/hr) −1.446e+09 −2.535e+09 −2.538e+09 −3.105e+09 −8.518e+08 -
TABLE 5 Stream Compositions Name 200 204 206 220 Comp Mole Frac 0.0000* 0.0000 0.0000 0.0000 (H2S) Comp Mole Frac 0.0051* 0.0051 0.0016 0.0051 (Nitrogen) Comp Mole Frac 0.6308* 0.6308 0.8168 0.6316 (CO2) Comp Mole Frac 0.3570* 0.3570 0.1680 0.3576 (Methane) Comp Mole Frac 0.0037* 0.0037 0.0037 0.0037 (Ethane) Comp Mole Frac 0.0013* 0.0013 0.0020 0.0013 (Propane) Comp Mole Frac 0.0002* 0.0002 0.0004 0.0001 (i-Butane) Comp Mole Frac 0.0005* 0.0005 0.0011 0.0003 (n-Butane) Comp Mole Frac 0.0000* 0.0000 0.0000 0.0000 (i-Pentane) Comp Mole Frac 0.0000* 0.0000 0.0000 0.0000 (n-Pentane) Comp Mole Frac 0.0007* 0.0007 0.0028 0.0002 (n-Hexane) Comp Mole Frac 0.0008* 0.0008 0.0037 0.0001 (n -Octane) Comp Mole Frac 0.0000* 0.0000 0.0000 0.0000 (H2O) Name 214 212 202 218 Comp Mole Frac 0.0000 0.0000 0.0000 0.0000 (H2S) Comp Mole Frac 0.0016 0.0000 0.0051 0.0016 (Nitrogen) Comp Mole Frac 0.8229 0.0700 0.6308 0.8229 (CO2) Comp Mole Frac 0.1693 0.0000 0.3570 0.1693 (Methane) Comp Mole Frac 0.0037 0.0000 0.0037 0.0037 (Ethane) Comp Mole Frac 0.0018 0.0302 0.0013 0.0018 (Propane) Comp Mole Frac 0.0001 0.0252 0.0002 0.0001 (i-Butane) Comp Mole Frac 0.0003 0.0949 0.0005 0.0003 (n-Butane) Comp Mole Frac 0.0000 0.0000 0.0000 0.0000 (i-Pentane) Comp Mole Frac 0.0000 0.0000 0.0000 0.0000 (n-Pentane) Comp Mole Frac 0.0001 0.3260 0.0007 0.0001 (n-Hexane) Comp Mole Frac 0.0000 0.4537 0.0008 0.0000 (n-Octane) Comp Mole Frac 0.0000 0.0000 0.0000 0.0000 (H2O) Name 224 230 240 232 Comp Mole Frac 0.0000 0.0000 0.0000 0.0000 (H2S) Comp Mole Frac 0.0051 0.0094 0.0000 0.0094 (Nitrogen) Comp Mole Frac 0.6316 0.3586 0.9500 0.3586 (CO2) Comp Mole Frac 0.3576 0.6275 0.0428 0.6275 (Methane) Comp Mole Frac 0.0037 0.0041 0.0032 0.0041 (Ethane) Comp Mole Frac 0.0013 0.0004 0.0023 0.0004 (Propane) Comp Mole Frac 0.0001 0.0000 0.0003 0.0000 (i-Butane) Comp Mole Frac 0.0003 0.0000 0.0007 0.0000 (n-Butane) Comp Mole Frac 0.0000 0.0000 0.0000 0.0000 (i-Pentane) Comp Mole Frac 0.0000 0.0000 0.0000 0.0000 (n-Pentane) Comp Mole Frac 0.0002 0.0000 0.0005 0.0000 (n-Hexane) Comp Mole Frac 0.0001 0.0000 0.0002 0.0000 (n-Octane) Comp Mole Frac 0.0000 0.0000 0.0000 0.0000 (H2O) Name 234 244 242 220 216 Comp Mole Frac 0.0000 0.0000 0.0000 0.0000 0.0000 (H2S) Comp Mole Frac 0.0094 0.0000 0.0000 0.0059 0.0016 (Nitrogen) Comp Mole Frac 0.3586 0.9500 0.9500 0.5901 0.8229 (CO2) Comp Mole Frac 0.6275 0.0428 0.0428 0.3984 0.1693 (Methane) Comp Mole Frac 0.0041 0.0032 0.0032 0.0037 0.0037 (Ethane) Comp Mole Frac 0.0004 0.0023 0.0023 0.0011 0.0018 (Propane) Comp Mole Frac 0.0000 0.0003 0.0003 0.0001 0.0001 (i-Butane) Comp Mole Frac 0.0000 0.0007 0.0007 0.0003 0.0003 (n-Butane) Comp Mole Frac 0.0000 0.0000 0.0000 0.0000 0.0000 (i-Pentane) Comp Mole Frac 0.0000 0.0000 0.0000 0.0000 0.0000 (n-Pentane) Comp Mole Frac 0.0000 0.0005 0.0005 0.0002 0.0001 (n-Hexane) Comp Mole Frac 0.0000 0.0002 0.0002 0.0001 0.0000 (n-Octane) Comp Mole Frac 0.0000 0.0000 0.0000 0.0000 0.0000 (H2O) -
TABLE 6 Energy Streams Heat Flow Name (Btu/hr) 300 3.107e+07 302 2.138e+07 304 6.401e+06 306 7.371e+07 308 3.014e+07 314 2.890e+06 310 4.946e+06 - While preferred embodiments of the invention have been shown and described, modifications thereof can be made by one skilled in the art without departing from the spirit and teachings of the invention. The embodiments described herein are exemplary only, and are not intended to be limiting. Many variations and modifications of the invention disclosed herein are possible and are within the scope of the invention. Specifically, while the process is described in terms of a continuous process, it is contemplated that the process can be implemented as a batch process. In addition, where numerical ranges or limitations are expressly stated, such express ranges or limitations should be understood to include iterative ranges or limitations of like magnitude falling within the expressly stated ranges or limitations (e.g., from about 1 to about 10 includes, 2, 3, 4, etc.; greater than 0.10 includes 0.11, 0.12, 0.13, etc.). Use of the term “optionally” with respect to any element of a claim is intended to mean that the subject element is required, or alternatively, is not required. Both alternatives are intended to be within the scope of the claim. Use of broader terms such as comprises, includes, having, etc. should be understood to provide support for narrower terms such as consisting of, consisting essentially of, comprised substantially of, etc. Moreover, the percentages described herein may be mole fraction, weight fraction, or volumetric fraction.
- Accordingly, the scope of protection is not limited by the description set out above but is only limited by the claims which follow, that scope including all equivalents of the subject matter of the claims. Each and every claim is incorporated into the specification as an embodiment of the present invention. Thus, the claims are a further description and are an addition to the preferred embodiments of the present invention. The discussion of a reference in the herein is not an admission that it is prior art to the present invention, especially any reference that may have a publication date after the priority date of this application. The disclosures of all patents, patent applications, and publications cited herein are hereby incorporated by reference, to the extent that they provide exemplary, procedural or other details supplementary to those set forth herein.
Claims (34)
1. A method of treating a hydrocarbon feed stream comprising carbon dioxide, the method comprising:
separating a carbon dioxide-lean stream and a carbon dioxide-rich stream from a light hydrocarbon stream;
separating a reflux stream from the carbon dioxide-lean stream in a reflux condenser;
recycling the reflux stream to the separator;
cooling the light hydrocarbon stream using at least a portion of the carbon dioxide-lean stream; and
feeding at least a portion of the carbon dioxide-lean stream into a hydrocarbon sweetening process.
2. The process of claim 1 wherein the hydrocarbon feed stream is separated into the light hydrocarbon stream and a heavy hydrocarbon stream.
3. The process of claim 1 wherein the carbon dioxide-lean stream and the carbon dioxide-rich stream are separated from the light hydrocarbon stream by distillation.
4. The process of claim 3 wherein a packing material and trays are utilized in the distillation step.
5. The process of claim 1 further comprising changing the temperature of the carbon dioxide-lean stream after its separation from the light hydrocarbon stream and before it is fed into the hydrocarbon sweetening process.
6. The process of claim 1 wherein the hydrocarbon sweetening process comprises a SELEXOL process.
7. The process of claim 1 further comprising injecting a portion of the carbon dioxide-rich stream into a subterranean formation containing hydrocarbons.
8. The process of claim 7 further comprising removing hydrocarbons from the subterranean formation after the injection step.
9. The process of claim 1 further comprising:
changing the temperature of the carbon dioxide-lean stream after its separation from the light hydrocarbon stream and before it is fed into the SELEXOL process; and
wherein the carbon dioxide-lean stream and the carbon dioxide-rich stream are separated from the light hydrocarbon stream by distillation comprising packing material and trays.
10. The process of claim 1 wherein the carbon dioxide-lean stream has a different composition after its separation from the light hydrocarbon stream and before it is fed into the hydrocarbon sweetening process.
11. A process for treating a feed mixture comprising hydrocarbons and carbon dioxide comprising:
removing at least some heavy hydrocarbons from the feed mixture;
separating from the feed mixture a first effluent leaner in carbon dioxide than the feed mixture and a second effluent richer in carbon dioxide than the feed mixture;
exchanging heat between at least a portion of the first effluent and the feed mixture;
condensing a portion of the first effluent;
recycling the condensed portion of the first effluent into the feed mixture; and
delivering the uncondensed portion of the first effluent to a hydrocarbon sweetening process.
12. The process of claim 11 wherein the heavy hydrocarbons comprise butane and heavier hydrocarbons.
13. The process of claim 11 further comprising injecting a portion of the second effluent into a subterranean formation comprising hydrocarbons.
14. The process of claim 13 further comprising removing hydrocarbons from the subterranean formation after the injection step.
15. The process of claim 11 wherein the separation step is carried out in a distillation column.
16. The process of claim 15 wherein the first effluent is condensed in a reflux condenser.
17. The process of claim 15 wherein the distillation column comprises a packing material and a plurality of trays.
18. The process of claim 11 comprising cooling a portion of the second effluent.
19. The process of claim 18 wherein the second effluent is cooled with a refrigerant.
20. The process of claim 18 wherein the second effluent is cooled with a process stream.
21. The process of claim 18 further comprising injecting a portion of the second effluent into a subterranean formation comprising hydrocarbons.
22. The process of claim 21 further comprising removing hydrocarbons from the subterranean formation after the injection step.
23. The process of claim 22 wherein the second effluent is cooled with a cold fluid.
24. The process of claim 23 wherein the heavy hydrocarbons comprise butane and heavier hydrocarbons.
25. The process of claim 24 wherein the uncondensed portion of the first effluent comprises at least 60% methane.
26. The process of claim 24 wherein the second effluent comprises greater than 90% carbon dioxide.
27. The process of claim 11 wherein the uncondensed portion of the first effluent comprises at least 60% methane.
28. The process of claim 11 wherein the second effluent comprises greater than 90% carbon dioxide.
29. A process for treating a hydrocarbon feed stream comprising:
separating the hydrocarbon feed stream into a light hydrocarbon stream and a heavy hydrocarbon stream;
a step for forming a heavy effluent stream and a light effluent stream from the light hydrocarbon stream;
separating a reflux stream and a carbon dioxide-lean stream from the light effluent stream;
separating a recycle stream and a carbon dioxide-rich stream from the heavy effluent stream;
cooling the light hydrocarbon stream with the carbon dioxide-lean stream; and
feeding the carbon dioxide-lean stream to a SELEXOL process.
30. The process of claim 29 further comprising feeding the carbon dioxide-rich stream to a pipeline.
31. The process of claim 29 wherein the step for forming a heavy effluent stream and a light effluent stream comprises treatment of the light hydrocarbon stream in a distillation column.
32. The process of claim 31 wherein the reflux stream and carbon dioxide-lean stream are separated from the light effluent stream in a reflux condenser.
33. A process for treating a hydrocarbon feed stream containing carbon dioxide comprising:
treating the hydrocarbon feed stream in a distillation column to produce a carbon dioxide-lean first column stream and a carbon dioxide-rich second column stream;
treating the first column stream in a reflux condenser to produce a reflux stream and a carbon dioxide-lean output stream;
recycling the reflux stream into the distillation column;
cooling the hydrocarbon feed stream with at least a portion of the carbon dioxide-lean output stream; and
feeding at least a portion of the carbon dioxide-lean output stream into a hydrocarbon sweetening process.
34. The process of claim 33 wherein a heavy hydrocarbon stream is separated from the hydrocarbon feed stream prior to treating the hydrocarbon feed stream in the distillation column.
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Families Citing this family (19)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US9752826B2 (en) | 2007-05-18 | 2017-09-05 | Pilot Energy Solutions, Llc | NGL recovery from a recycle stream having natural gas |
JP4981771B2 (en) * | 2008-09-08 | 2012-07-25 | 三菱重工業株式会社 | Coal gasification combined power generation facility |
US8334418B2 (en) * | 2008-11-05 | 2012-12-18 | Water Generating Systems LLC | Accelerated hydrate formation and dissociation |
EP2210656A1 (en) * | 2009-01-27 | 2010-07-28 | General Electric Company | Hybrid carbon dioxide separation process and system |
JP5566448B2 (en) | 2009-03-25 | 2014-08-06 | フルオー・テクノロジーズ・コーポレイシヨン | Improved arrangement and method for removing high pressure acid gases |
DE102009017228A1 (en) * | 2009-04-09 | 2010-10-14 | Linde-Kca-Dresden Gmbh | Process and device for the treatment of flue gases |
CA2693640C (en) * | 2010-02-17 | 2013-10-01 | Exxonmobil Upstream Research Company | Solvent separation in a solvent-dominated recovery process |
CA2696638C (en) * | 2010-03-16 | 2012-08-07 | Exxonmobil Upstream Research Company | Use of a solvent-external emulsion for in situ oil recovery |
CA2705643C (en) | 2010-05-26 | 2016-11-01 | Imperial Oil Resources Limited | Optimization of solvent-dominated recovery |
CN102166463B (en) * | 2011-03-21 | 2013-03-13 | 海湾环保工程(北京)股份有限公司 | Simulation test device for recovering volatile organic gases |
US20150152722A1 (en) * | 2012-11-29 | 2015-06-04 | Paul Andrew Carmody | System and method for realizing added value from production gas streams in a carbon dioxide flooded eor oilfield |
CA2899136A1 (en) * | 2013-01-25 | 2014-07-31 | H R D Corporation | Method of high shear comminution of solids |
WO2014130837A1 (en) * | 2013-02-21 | 2014-08-28 | Jianguo Xu | Co2 capture from co2-rich natural gas |
US10254042B2 (en) | 2013-10-25 | 2019-04-09 | Air Products And Chemicals, Inc. | Purification of carbon dioxide |
GB2521177B (en) * | 2013-12-11 | 2020-09-23 | Costain Oil Gas & Process Ltd | Process and apparatus for separation of carbon dioxide and hydrocarbons |
US20150251134A1 (en) * | 2014-03-10 | 2015-09-10 | Uop Llc | Methods and apparatuses for removing impurities from a gaseous stream |
NO20150079A1 (en) * | 2015-01-17 | 2015-03-12 | Int Energy Consortium As | System for injecting flue gas to a subterranean formation |
WO2018147883A1 (en) | 2017-02-09 | 2018-08-16 | Fluor Technologies Corporation | Two-stage absorption for acid gas and mercaptan removal |
WO2018200694A1 (en) * | 2017-04-28 | 2018-11-01 | Dow Global Technologies Llc | Processes and systems for separating carbon dioxide in the production of alkanes |
Citations (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4130403A (en) * | 1977-08-03 | 1978-12-19 | Cooley T E | Removal of H2 S and/or CO2 from a light hydrocarbon stream by use of gas permeable membrane |
US4459142A (en) * | 1982-10-01 | 1984-07-10 | Standard Oil Company (Indiana) | Cryogenic distillative removal of CO2 from high CO2 content hydrocarbon containing streams |
US4563202A (en) * | 1984-08-23 | 1986-01-07 | Dm International Inc. | Method and apparatus for purification of high CO2 content gas |
USH825H (en) * | 1988-05-20 | 1990-10-02 | Exxon Production Research Company | Process for conditioning a high carbon dioxide content natural gas stream for gas sweetening |
US20050066815A1 (en) * | 2003-09-26 | 2005-03-31 | Consortium Services Management Group, Inc. | CO2 separator method and apparatus |
US20060042463A1 (en) * | 2004-08-31 | 2006-03-02 | Frantz Stephen R | High efficiency gas sweetening system and method |
Family Cites Families (89)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US825A (en) * | 1838-07-09 | Bail way cooking-stove | ||
US2996891A (en) | 1957-09-23 | 1961-08-22 | Conch Int Methane Ltd | Natural gas liquefaction cycle |
US3242681A (en) | 1963-01-31 | 1966-03-29 | Philips Corp | Natural gas liquefaction and storage |
US4171964A (en) | 1976-06-21 | 1979-10-23 | The Ortloff Corporation | Hydrocarbon gas processing |
US4157904A (en) | 1976-08-09 | 1979-06-12 | The Ortloff Corporation | Hydrocarbon gas processing |
US4251249A (en) | 1977-01-19 | 1981-02-17 | The Randall Corporation | Low temperature process for separating propane and heavier hydrocarbons from a natural gas stream |
US4152129A (en) | 1977-02-04 | 1979-05-01 | Trentham Corporation | Method for separating carbon dioxide from methane |
US4185978A (en) | 1977-03-01 | 1980-01-29 | Standard Oil Company (Indiana) | Method for cryogenic separation of carbon dioxide from hydrocarbons |
US4278457A (en) | 1977-07-14 | 1981-07-14 | Ortloff Corporation | Hydrocarbon gas processing |
US4318723A (en) | 1979-11-14 | 1982-03-09 | Koch Process Systems, Inc. | Cryogenic distillative separation of acid gases from methane |
US4350511A (en) * | 1980-03-18 | 1982-09-21 | Koch Process Systems, Inc. | Distillative separation of carbon dioxide from light hydrocarbons |
CA1169012A (en) | 1980-10-16 | 1984-06-12 | Walter C.G. Kosters | Process for the simultaneous separation in aromatics and non-aromatics of a heavy hydrocarbon stream and a light hydrocarbon stream |
US4322225A (en) | 1980-11-04 | 1982-03-30 | Phillips Petroleum Company | Natural gas processing |
US4370156A (en) | 1981-05-29 | 1983-01-25 | Standard Oil Company (Indiana) | Process for separating relatively pure fractions of methane and carbon dioxide from gas mixtures |
US4466946A (en) * | 1982-03-12 | 1984-08-21 | Standard Oil Company (Indiana) | CO2 Removal from high CO2 content hydrocarbon containing streams |
US4529411A (en) | 1982-03-12 | 1985-07-16 | Standard Oil Company | CO2 Removal from high CO2 content hydrocarbon containing streams |
US4441900A (en) | 1982-05-25 | 1984-04-10 | Union Carbide Corporation | Method of treating carbon-dioxide-containing natural gas |
US4519824A (en) | 1983-11-07 | 1985-05-28 | The Randall Corporation | Hydrocarbon gas separation |
US4639257A (en) * | 1983-12-16 | 1987-01-27 | Costain Petrocarbon Limited | Recovery of carbon dioxide from gas mixture |
US4681612A (en) | 1984-05-31 | 1987-07-21 | Koch Process Systems, Inc. | Process for the separation of landfill gas |
DE3515949A1 (en) | 1984-06-14 | 1985-12-19 | Linde Ag, 6200 Wiesbaden | METHOD FOR SEPARATING CO (DOWN ARROW) 2 (DOWN ARROW) FROM A GAS MIXTURE |
US4557911A (en) * | 1984-06-28 | 1985-12-10 | Amoco Corporation | Process for producing sweet CO2 and hydrocarbon streams |
FR2571129B1 (en) | 1984-09-28 | 1988-01-29 | Technip Cie | PROCESS AND PLANT FOR CRYOGENIC FRACTIONATION OF GASEOUS LOADS |
US4617039A (en) | 1984-11-19 | 1986-10-14 | Pro-Quip Corporation | Separating hydrocarbon gases |
FR2578637B1 (en) | 1985-03-05 | 1987-06-26 | Technip Cie | PROCESS FOR FRACTIONATION OF GASEOUS LOADS AND INSTALLATION FOR CARRYING OUT THIS PROCESS |
DE3510097A1 (en) | 1985-03-20 | 1986-09-25 | Linde Ag, 6200 Wiesbaden | METHOD FOR SEPARATING CO (DOWN ARROW) 2 (DOWN ARROW) FROM A GAS MIXTURE |
US4602477A (en) * | 1985-06-05 | 1986-07-29 | Air Products And Chemicals, Inc. | Membrane-aided distillation for carbon dioxide and hydrocarbon separation |
US4687499A (en) | 1986-04-01 | 1987-08-18 | Mcdermott International Inc. | Process for separating hydrocarbon gas constituents |
US4654062A (en) * | 1986-07-11 | 1987-03-31 | Air Products And Chemicals, Inc. | Hydrocarbon recovery from carbon dioxide-rich gases |
US4854955A (en) | 1988-05-17 | 1989-08-08 | Elcor Corporation | Hydrocarbon gas processing |
US4869740A (en) | 1988-05-17 | 1989-09-26 | Elcor Corporation | Hydrocarbon gas processing |
US4889545A (en) | 1988-11-21 | 1989-12-26 | Elcor Corporation | Hydrocarbon gas processing |
US5114451A (en) | 1990-03-12 | 1992-05-19 | Elcor Corporation | Liquefied natural gas processing |
US5064525A (en) | 1991-02-19 | 1991-11-12 | Uop | Combined hydrogenolysis plus oxidation process for sweetening a sour hydrocarbon fraction |
US5275005A (en) | 1992-12-01 | 1994-01-04 | Elcor Corporation | Gas processing |
US5568737A (en) | 1994-11-10 | 1996-10-29 | Elcor Corporation | Hydrocarbon gas processing |
US5779507A (en) | 1995-05-15 | 1998-07-14 | Yeh; Te-Hsin | Terminal device for interface sockets |
BR9609099A (en) | 1995-06-07 | 1999-02-02 | Elcor Corp | Process and device for separating a gas stream |
US5555748A (en) | 1995-06-07 | 1996-09-17 | Elcor Corporation | Hydrocarbon gas processing |
US5799507A (en) | 1996-10-25 | 1998-09-01 | Elcor Corporation | Hydrocarbon gas processing |
US5983664A (en) | 1997-04-09 | 1999-11-16 | Elcor Corporation | Hydrocarbon gas processing |
US5890378A (en) | 1997-04-21 | 1999-04-06 | Elcor Corporation | Hydrocarbon gas processing |
US5881569A (en) | 1997-05-07 | 1999-03-16 | Elcor Corporation | Hydrocarbon gas processing |
US5983663A (en) | 1998-05-08 | 1999-11-16 | Kvaerner Process Systems, Inc. | Acid gas fractionation |
US6182469B1 (en) | 1998-12-01 | 2001-02-06 | Elcor Corporation | Hydrocarbon gas processing |
US6244070B1 (en) | 1999-12-03 | 2001-06-12 | Ipsi, L.L.C. | Lean reflux process for high recovery of ethane and heavier components |
FR2808223B1 (en) * | 2000-04-27 | 2002-11-22 | Inst Francais Du Petrole | PROCESS FOR THE PURIFICATION OF AN EFFLUENT CONTAINING CARBON GAS AND HYDROCARBONS BY COMBUSTION |
US6755965B2 (en) | 2000-05-08 | 2004-06-29 | Inelectra S.A. | Ethane extraction process for a hydrocarbon gas stream |
AU7158701A (en) | 2000-08-11 | 2002-02-25 | Fluor Corp | High propane recovery process and configurations |
US20020166336A1 (en) | 2000-08-15 | 2002-11-14 | Wilkinson John D. | Hydrocarbon gas processing |
EP1322897A2 (en) | 2000-10-02 | 2003-07-02 | Elkcorp | Hydrocarbon gas processing |
US6526777B1 (en) | 2001-04-20 | 2003-03-04 | Elcor Corporation | LNG production in cryogenic natural gas processing plants |
US6742358B2 (en) | 2001-06-08 | 2004-06-01 | Elkcorp | Natural gas liquefaction |
US6945075B2 (en) | 2002-10-23 | 2005-09-20 | Elkcorp | Natural gas liquefaction |
US20040099138A1 (en) * | 2002-11-21 | 2004-05-27 | L'air Liquide, Societe Anonyme A Directoire Et Conseil De Surveillance Pour L'etude Et | Membrane separation process |
KR101120324B1 (en) | 2003-02-25 | 2012-06-12 | 오르트로프 엔지니어스, 리미티드 | Hydrocarbon gas processing |
US6889523B2 (en) | 2003-03-07 | 2005-05-10 | Elkcorp | LNG production in cryogenic natural gas processing plants |
US7155931B2 (en) | 2003-09-30 | 2007-01-02 | Ortloff Engineers, Ltd. | Liquefied natural gas processing |
US7124605B2 (en) * | 2003-10-30 | 2006-10-24 | National Tank Company | Membrane/distillation method and system for extracting CO2 from hydrocarbon gas |
US7159417B2 (en) | 2004-03-18 | 2007-01-09 | Abb Lummus Global, Inc. | Hydrocarbon recovery process utilizing enhanced reflux streams |
US7204100B2 (en) | 2004-05-04 | 2007-04-17 | Ortloff Engineers, Ltd. | Natural gas liquefaction |
NZ549467A (en) | 2004-07-01 | 2010-09-30 | Ortloff Engineers Ltd | Liquefied natural gas processing |
US9080810B2 (en) | 2005-06-20 | 2015-07-14 | Ortloff Engineers, Ltd. | Hydrocarbon gas processing |
US7666251B2 (en) | 2006-04-03 | 2010-02-23 | Praxair Technology, Inc. | Carbon dioxide purification method |
CN101460800B (en) | 2006-06-02 | 2012-07-18 | 奥特洛夫工程有限公司 | Liquefied natural gas processing |
US20080078205A1 (en) | 2006-09-28 | 2008-04-03 | Ortloff Engineers, Ltd. | Hydrocarbon Gas Processing |
US7777088B2 (en) * | 2007-01-10 | 2010-08-17 | Pilot Energy Solutions, Llc | Carbon dioxide fractionalization process |
US8590340B2 (en) | 2007-02-09 | 2013-11-26 | Ortoff Engineers, Ltd. | Hydrocarbon gas processing |
US9869510B2 (en) | 2007-05-17 | 2018-01-16 | Ortloff Engineers, Ltd. | Liquefied natural gas processing |
US8919148B2 (en) | 2007-10-18 | 2014-12-30 | Ortloff Engineers, Ltd. | Hydrocarbon gas processing |
US20090282865A1 (en) | 2008-05-16 | 2009-11-19 | Ortloff Engineers, Ltd. | Liquefied Natural Gas and Hydrocarbon Gas Processing |
US8584488B2 (en) | 2008-08-06 | 2013-11-19 | Ortloff Engineers, Ltd. | Liquefied natural gas production |
US8881549B2 (en) | 2009-02-17 | 2014-11-11 | Ortloff Engineers, Ltd. | Hydrocarbon gas processing |
US9939195B2 (en) | 2009-02-17 | 2018-04-10 | Ortloff Engineers, Ltd. | Hydrocarbon gas processing including a single equipment item processing assembly |
US9080811B2 (en) | 2009-02-17 | 2015-07-14 | Ortloff Engineers, Ltd | Hydrocarbon gas processing |
US9933207B2 (en) | 2009-02-17 | 2018-04-03 | Ortloff Engineers, Ltd. | Hydrocarbon gas processing |
US9074814B2 (en) | 2010-03-31 | 2015-07-07 | Ortloff Engineers, Ltd. | Hydrocarbon gas processing |
US9052137B2 (en) | 2009-02-17 | 2015-06-09 | Ortloff Engineers, Ltd. | Hydrocarbon gas processing |
MX341798B (en) | 2009-02-17 | 2016-09-02 | Ortloff Engineers Ltd | Hydrocarbon gas processing. |
US9052136B2 (en) | 2010-03-31 | 2015-06-09 | Ortloff Engineers, Ltd. | Hydrocarbon gas processing |
US8434325B2 (en) | 2009-05-15 | 2013-05-07 | Ortloff Engineers, Ltd. | Liquefied natural gas and hydrocarbon gas processing |
US20100287982A1 (en) | 2009-05-15 | 2010-11-18 | Ortloff Engineers, Ltd. | Liquefied Natural Gas and Hydrocarbon Gas Processing |
AU2010259046A1 (en) | 2009-06-11 | 2012-02-23 | Ortloff Engineers, Ltd. | Hydrocarbon gas processing |
US20110067441A1 (en) | 2009-09-21 | 2011-03-24 | Ortloff Engineers, Ltd. | Hydrocarbon Gas Processing |
US9021832B2 (en) | 2010-01-14 | 2015-05-05 | Ortloff Engineers, Ltd. | Hydrocarbon gas processing |
US9068774B2 (en) | 2010-03-31 | 2015-06-30 | Ortloff Engineers, Ltd. | Hydrocarbon gas processing |
US9057558B2 (en) | 2010-03-31 | 2015-06-16 | Ortloff Engineers, Ltd. | Hydrocarbon gas processing including a single equipment item processing assembly |
MY160789A (en) | 2010-06-03 | 2017-03-15 | Ortloff Engineers Ltd | Hydrocarbon gas processing |
US8861148B2 (en) * | 2010-07-29 | 2014-10-14 | Lennox Industries Inc. | Surge protector, an HVAC unit including the surge protector and a method of testing electrical equipment |
-
2007
- 2007-01-10 US US11/621,913 patent/US7777088B2/en not_active Ceased
-
2008
- 2008-01-07 WO PCT/US2008/050364 patent/WO2008086265A1/en active Application Filing
-
2010
- 2010-06-28 US US12/824,382 patent/US8709215B2/en active Active
-
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- 2013-01-07 US US13/735,646 patent/USRE44462E1/en not_active Expired - Fee Related
- 2013-10-09 US US14/049,744 patent/US8816148B2/en active Active
-
2014
- 2014-03-07 US US14/200,346 patent/US9481834B2/en active Active
-
2016
- 2016-10-31 US US15/339,610 patent/US10316260B2/en active Active
Patent Citations (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US4130403A (en) * | 1977-08-03 | 1978-12-19 | Cooley T E | Removal of H2 S and/or CO2 from a light hydrocarbon stream by use of gas permeable membrane |
US4459142A (en) * | 1982-10-01 | 1984-07-10 | Standard Oil Company (Indiana) | Cryogenic distillative removal of CO2 from high CO2 content hydrocarbon containing streams |
US4563202A (en) * | 1984-08-23 | 1986-01-07 | Dm International Inc. | Method and apparatus for purification of high CO2 content gas |
USH825H (en) * | 1988-05-20 | 1990-10-02 | Exxon Production Research Company | Process for conditioning a high carbon dioxide content natural gas stream for gas sweetening |
US20050066815A1 (en) * | 2003-09-26 | 2005-03-31 | Consortium Services Management Group, Inc. | CO2 separator method and apparatus |
US20060042463A1 (en) * | 2004-08-31 | 2006-03-02 | Frantz Stephen R | High efficiency gas sweetening system and method |
Cited By (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US10316260B2 (en) | 2007-01-10 | 2019-06-11 | Pilot Energy Solutions, Llc | Carbon dioxide fractionalization process |
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US20170044449A1 (en) | 2017-02-16 |
US9481834B2 (en) | 2016-11-01 |
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US20140183101A1 (en) | 2014-07-03 |
US8709215B2 (en) | 2014-04-29 |
US7777088B2 (en) | 2010-08-17 |
US20100258401A1 (en) | 2010-10-14 |
US8816148B2 (en) | 2014-08-26 |
US20080167511A1 (en) | 2008-07-10 |
USRE44462E1 (en) | 2013-08-27 |
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